Starting and controlling contacting operations



Dec. 16, 1941. J. w. HARRlsoN -Er-,AL

STARTING AND coNTRoLLING UONTAGTING OPERATIONS Filed sept. 2:5, 1939 INVEN-roRs ./AMEs m #ARR/som rle/ms e. @Rickert ATTORNEY l Patented Dec. 16, 19.41

UNITED STATES PATENT oFFIcE STARTING AND CONTROLLING C ONTACTIN G GPERATIONS James W. Harrison, Woodbury, N. J., and Thomas B. Prickett, Philadelphia, Pa., assignors to Houdry Process Corporation, Wilmington, Del., a corporation of Delaware Application september .23, 1939, serial 10,296,184

v (ci. 19e-52) Claims oxidation in order` to condition thevmaterial for the following treating or on-stream period of the cycle, heat is evolved which increases the temperature of the conta'ct material and associated converter structure which must be controlled in order to prevent injury to the mass and converter parts.

Various methods have heretofore been devised for controlling the temperature of and maintaining the contact material and the associated converter structure, comprising the converter walls, tube sheets and various tubes with or Without heat exchange fins, at the required temperatures for the diierent reactions. One highly successful operation is by utilizing an extraneous heat exchange medium to add heat during the endothermic period of the cycle and to withdraw the heat evolved during the exothermic period of the cycle in order to maintain the contact material at the desired on-stream temperature during one period and to maintain the mass at a temperature suiciently high during the alternate period to hasten the exothermic or regeneration reaction and yet during this latter reaction to maintain the temperature sufficiently low or controlled so that injury to the converter structure or contact mass will be prevented. This alternate heating up and cooling down of the mass in changing from one period of the cycle to another tends to prolong the op. erating cycle and to make it thereby somewhat uneconomical.

Objects of the present invention therefore are directed to anew and emcient manner of using an extraneous heat exchange medium in con- Y highly heated condition through the heat Ae'ill- -and in certain respects more positive and eilitrolling the temperature of the reactions; to reduce the operating cycle and control' the operations, soas to produce economically, higher yields of products; to provide a highly eiiicient use of the heat storage capacity of the converter structure and contact mass; to utilize the evolved heat of reaction substantially continuously throughout the cycle of operation a novel and efficient manner; to provide for the positive conn trolV of thetemperature of the heat exchange medium entering the converters; to provide for greater flexibility in controlling the temperature of the entering reactants; and to provide for heating up the contact'material and converter structure to reaction temperature in a minimum of time.

This invention may be considered to be an improvement over, a variant of, or a further development of the invention disclosed in the copend- Y ing application of Clarence H. Thayer, Serial Number 183,305, filed January 4,1938, for Starting up and temperature control of contact operations, which invention is directed to the idea of raising the temperature of the contact material and associated converter structure-by passing heated air through the contact material to raise its temperature several hundred degrees and then passing heat exchange medium in change conduits to raise the temperature ci! the materias to substantially reaction temperature: controlling the temperature of the mass for the alternate reactions by admitting the extraneous heat exchange medium at a temperature intermediate the different reaction temperatures for passage through the heat exchange conduits A1ocated within the mass, as well as controlling the temperature of the heat exchange uid so that it enters the heat exchange conduits at a substantially constant temperature by using a small portion of the main body of heat exchange Afluid in heat exchange vyithvthe incoming oil charge or other reactants before returning and mixing the portion with the main body o f the heat ex'- change iiuid.' The present invention attains the results accomplished by the invention disclosed in the above mentioned application in a diierent cient manner by simultaneously passing heated air through the contact mass and heat exchange conduits and consequently heating up the mass and associated structure more quickly; by supplying the extraneous heat exchange fluid at a constant temperature which is below or near that of the lower reaction temperature so as to withdraw practically continuously the exothermic heat of reaction during the cycle of. alternating reactions; and in controlling the temperature of the heat exchange'iluid 'entering the converters by passing a portion thereof in heat exchange relation with the incoming oil charge in a manner which insures the proper heating of any particular charge.

The single igure of the drawing is a diagrammatic elevational view of one arrangement of apparatus with one of the converters sectioned to show the details.

Y The two converters which are indicated at A and B are merely representative of the number which may be used in carrying out the invention. It will be clear from the detailed .description which follows that the invention is applicable to one converter for'carrying out the different reactions in alternation or to any number of converters for simultaneously carrying out the alternate reactions in dierent converters. Each of the converters has a reaction chamber .III as indicated in the sectioned converter, which contains a contact mass M, usually in the form of small pieces, fragments or molded pellets and which are capable of regeneration in situ. Any

- consist ofadsorptive, silicious or clayey material andmay comprise ablend or compound of silica with another metalliferous material such as alumina and may or Vmay not have small amounts of other active materials or regeneration promoters. C indicates a combustion case having a reaction chamber and associated structural parts which are similar to those of the converters A or B. Only one combustion case is shown but any desired number may be used, depending on the number of reaction converters. used in the plant. The reaction chamber of the combustion case contains a contact mass of a different type from that used in the converters and may comprise copper oxide or other suitable material, such as oxides or compounds of iron cobalt, nickel and lead, usually on a suitable support or carrier.

As shown in the sectionedv converter A. manifolds are provided for supplying reactants to and V removing reaction products from the reaction chamber and other manifolds are provided for i supplying and removing heat exchange fluid. The

converters may have one manifold II at the top adjacent the reaction chamber and a manifold I2 below and adiacent the chamber which are used in supplying reactants to and removing reaction productsV from the reaction chamber through nested conduit assemblies I3, the outer conduit being perforated, and through the perforated conduits I4, which are vin fluid communication with one or the other of these manifolds. The heat exchange fluid manifolds I and I6 may, as shown, be positioned directly below the manifold I2 and in fluid communication with inner and outer nested heat exchange fluid conduits I1 and I8, respectively, for passing ahheat exchange fluid in indirect heat exchange rela-l tion with the contact mass.

The heat exchange fluid for controlling the temperature of the contact mass may comprise various fused salts or salt mixtures, molten metals of suitably low melting point, etc. and willbe illustrated by a fused salt mixture of sodium nitrate and potassium nitrite of approximately eutectic proportions. In order to clarify the description, the flow of the fused salt through the -varlous circuits is indicated by feathered arrows.

of alternate reactions it will substantially continuously pick up heat from the contact material and converter parts and may be circulated from tank I9 by means'of pump 20 and -follow line 2| to header 22, from which it is admitted to the lower heat exchange fluid manifolds I5 of the converters A and B through branches 23, and

heat exchange conduits I1 and through the outer conduits I8 into the heatexchange manifold I6 and return to the salt tank I9 through lines 24 andheader- 25. Thesalt in the tank I9 can be maintained at the desired constant temperature by extracting the heat picked up, which may be done by diverting from the tank any selected portion and heat exchanging this portion with other materials, for example, a predetermined portion may pass from the tank through line 26 to line 21 where it may be directed to one or both of the pumps 28 and 29 by proper manipulation of valves 30 and 3|. The diverted portion of the liquid may be used as a heat exchange medium for any desired purpose but, as shown in the drawing, it is used to control either the temperature of the oil charge incoming through line 32 an`d oil exchangers 33 before the oil is admitted to the reaction converters, or it may pass through boiler 34 and be used entirely in making steam, or it may pass in parallel with the exchangers 33 and boiler 34.

In a preferred aspect of the invention the salt stream is divided when it reaches line 21 and a portion is sent through exchangers 33 and another portion is sent in parallel through boiler 34 and both portions are picked up in line 35 and returned through line 36 to the tank I9. The particular arrangement of dividing this salt stream and sending it in parallel in heat exchange relation with a plurality of materials per- Inits greater exibility in the control of the temperature of the heat exchange fluid which is returned to the mixing tank and is better adapted for regulating the temperature of various incoming reactants and also provides a more positive control of the temperature of these fluids. The valves 30 and 3| permit regulated portions of the .fluid to pass through either exchangers 33 or boiler 34 and these portions may be -selected in accordance with the temperature at which it is desired to send the particular oil charge into the converters, or with the amount of steam it is desired to convert in boiler 34. A steam accumulator is shown in communication with boiler 34 for storing excess steam.

The present invention is concerned with conditioning or heating the contact material to a proper temperature for the reactions and maintaining the contact material at the proper temperatures throughout the operation of the appa- I ratus. Either' manifold or I2 may be used for distributing the incoming reactants while the remaining manifold will be used for collecting the products of the reaction. It is to be understood. however, that the invention is of value in controlling all alternating chemical reactions which are effected by or with the aid of contact masses and wherein during one'of the reactions a burnable deposit is formed on the contact mass, and during the other reactionheat is evolved through oxidation of the deposit formed on the mass.

For the purpose of illustrating the invention, assume the bodies of contact mass in the converters A and B to be used alternately in the aaeaosa transformation of a petroleum fraction boiling above or to a substantial extent above the gasoline boiling range, as for example a light gas oil having an end boiling point of approximately 750 F., and in regenerating the contact mass of deposit formed thereon duringthe transforming or on-stream reaction. The on-strea'm reaction, which is endothermic, will be carried out at temperatures between 750 Aand 925 F. and preferably at temperatures between 825 and 875 F. while the regeneration or `exothermic period of the cycle will start at about 825 F. and the contact mass will be maintained at a temperature low enough to prevent injury to the mass or converter parts during the strongest phase of the reaction and reducedin temperature by the salt to around 900 F. toward the end of the reaction. A stream of salt from the tank I9 will be sent in indirect heat exchange relation with the contact mass M of each converter A and B through the nested heat exchange conduits at a temperature preferably as low as the lower limits of the on-stream reactionand at least For example, the salt passing through the boiler below the average temperature of the on-stream period or, in the case o the specific gas oil above mentioned, the salt will be admitted between 800 and 850 F. or for example 825 F.

-as it passes in heat exchange relation with the mass which is undergoing regeneration, the heat exchange uid will pick up a substantial amount of heat and leave the mass at an increased temperature of approximately l0 to 30 F., depending upon the amount of burnable deposit laid down. The contact mass, which had previously been regenerated and is now at the temperature obtaining'at the end of the regeneration period or approximately 900 F., is further reduced in temperature by the endothermic heat of reac,

tion during the on-stream period and the salt, which passes in indirect heat exchange relation with this contact mass, also extracts the stored heat from the mass and associated structure during the reaction and further reduces the temperature -gradually to around the lower limit of the on-stream reaction or about 835 F. when the on-stream reactant is a light gas oil, as heretofore mentioned. During the passage of the salt through the body of contact material which is on stream, the salt increases in temperature in an amount somewhat below that of the salt passing through vthe mass during regeneration and leaves the converter with a temperature increase of from 2 to 15. The streams of heat exchange fluid after leavingthe converters A and B enter'the manifold 25, and pass to the salt tank I9 at a temperature of between 10 and 45 higher than the salt passing from the tank to the converters. A portion of the heat exchange liquid in tank I9 is then withdrawn' through line 26 to line 21 and passes therefrom in heat exchange relation in parallel with the oil exchangers' 33 and the boiler 34 so that this salt can be returned' to the tank at a -temperature low enough to adjust the main body of the heat exchange fluid in the tank to the temperature at which it isdesired to admit the -saltV to the converters. The rate and amount of salt Apassing through the exchangers 33 will be determined according to the particular charging stock and the temperature at which the charge is to enter the converters, while thel rate and.

amount of salt passing through the boiler 34 -will be in the neighborhood of 800 F. and by controllingl the temperature level at which the salt leaves the boiler, for example at about 650 F.. steam at above 400 pounds pressure and around 450 F., inl temperature may be formed, which is highly desirable in eflicient plant operation.

In anotheraspect this invention is concerned vwith heating up the apparatus to a temperature suilcient to start the reactions. If the contact material, tubes and other converter structure are a temperature ranging between 450 and 500 F.

This is done according to the present invention in a manner to maintain portions of the converter, such as the tube sheets and walls bounding the several manifolds at the same or substantially the same temperature by sending heated airinto the converters forsimultaneous passage through the contact material and salt circuit, so that the various converter parts will not be affectedv by uneven contraction and expansion. At the begin'- ning of the heating up period a compressor 40 is operated through a turbine 4I which is started by means of a motor 42 until sufficient air is compressed, circulated and returned to the turbine in condition to supply enough energy for operating the turbine without the aid of the motor. The

. circuit for the airthrough the apparatus for heating up -thecontact material and the converter structure and the circuit for the fumes which leave the converters during regeneration as well as the circuit for the oxidized fumes from the combustion case are indicated bythe arrowed o lines. The air is heated by compressor 40 and further heated, if necessary, by burner 43 to bettveenr450 and 500 F. and passes to line 44 and around the heat exchanger 38 through by-pass 45 to header 46 from which it passes through branches 4'I l into the inletmanifolds I2 of the converters and the combustion case From the manifolds I2 the air is distributed by the outer perforate tubes of the nested assemblies I3 through the contact masses and picked up by tubes I4 and carried to the upper manifolds II from which it is `directed to the header 48 through branches 49 which are in .communication with the manifolds I I of the converters and combustion case. From the-header. the cooled air is returned through line 50 to-a heater 5I, where it may be heated to a temperature to place it in condition for operating the turbine without the aid of the starting motor 42. Valved branches 52 leadfrom branch lines 4.1 to the heat exchange fluid lines 24 so that air may be admittedto a heat exchange fluid manifold of each of the converters and combustion case for passage through the heat exchange tubessimultaneously with the previously described .passage of air from the manifolds I2 through the contact masses. It is preferable, as indicated in the drawings, to supply'the air so that it passes first to the heat exchange fluid outlet manifolds I6 before passing through the heat exchange conduits II and I8 i to the inlet manifolds I5 but of course the air will depend on the steam requirements for plant A operation. The high temperature of the saltin tank I9 readily permits the formation in boiler` may rst enter the inlet manifolds I5 and pass through the tubes to the outer manifolds I 6. The

purpose of passing the heated air through this' portionof the saltcircuit is to maintain the partition or tube sheet betweenthe manifolds I2 and I6 and the walls of these manifolds at substanmanifolds I the cooled air will pass through branches 23 to the header 22 from which it may be permitted to escape through line 60 or returned to heater 5I through line 6I for passage to the turbine 4I. After the contact mass and the associated parts are heated to a temperature of approximately 450 to 500 F., thevalves in branches 52 will be closed so that no more air will be permitted to circulate in the heat exchange fluid circuit but the air which is gradually increased in temperature by burner 43 will continue to pass through the contact mass. At this time the salt in tank 19, which is maintained above its freezing point or in the neighborhood of 350 F., is then permitted to flow from the tank through the line, 2| by opening valve 39 and passesthrough heat exchanger 38 to be further heated by the air coming from the burner 43 to the header 22, the valve in by-pass 45 being closed to direct the air through this heat exchanger. A salt heater 54 is also provided in the line 2l beyond the air heat exchanger 38 for gradually increasing the temperature of the heat exchange fluid before being circulated through the heat exchange circuit back-to tank I9 so that the air and the salt are maintained at substantially the same temperatureswhile the respective uids are passing through the contact mass and through the heat exchange circuit and ing reaction for converting higher boiling hydrocarbons into lower boiling hydrocarbons and the alternate regeneration of the contact material following this reactionl is to be considered merely .as exemplary of the invention, vthe latter being limited only by the scope of the appended claims.

What we claim is:

1. In the treatment of reactant fluids in a reaction chamber used in a cycle of operation involving alternate periodsof greater exothermic reaction heat and lesser endothermic reaction heat and wherein a heat exchange uid is used to control the temperature of the reactions, the steps of circulating the heat exchange fluid at a constant temperature below that of the reactions in indirect heat exchange relation' with the reaction chamber, withdrawing only a portion of the evolved heat from the reaction chamber during the exothermic period by the heat exchange uid in order to permit the temperature of the reaction chamber to rise to a desired degree by storingheat therein, after a predeterperature before again beginning the cycle of permit the mass and the converter structure to gradually increase in temperature up to :around 650 F. and preferably around 8140 F. At this time the converters are ready to receive the onstream reactants for beginning the process cycle.

Whe-n the converters are properly heated up .;the valve in line 44 is closed to cut off thesupply of air to the contact material and the onstream reactants are sent into the reaction chambers A and B respectively, through valved 4lines 49a to manifolds I I and reaction products withdrawn through valved lines 41a from manifolds -I2, as

nary heating, salt may be passed through this portion of the circuit.

After the on-stream period of the cycle, as

heretofore mentioned, the contact material inthe converter or converters which4 have undergone' this period of the cycle is regenerated by passing an oxidizing medium through the material to burn oil' the deposit. The regeneration step is carried out by again supplying air, preferably heate-d'to about 800 F., to start the combustion of the deposits which continues as air is continually supplied until the 'burning is completed. The regeneration fumes collected in header 48 are passed directly through line 50 and heater 5I for operating the turbine 4I or sent through line 55 by closing valve 56 into combustion case C where CO and any other burnable jcomponents remaining in the fumes-are further' oxidized by the particular contact material thereoperation.

2. In the treatment of reactant uids in the presence of solid porous contact material used in-a cycle of operation involving alternate'perl- A ods of-greater exothermic reaction heat and lesser endothermic reaction heat and wherein a heat exchange fluid is used to control the temperature of the reactions, the steps' of circulating the heat exchange fluid during thecycle at a constant temperature below that of the reactions, in indirect heat exchange relation with the contact material, withdrawing only a portion in In order to increase their energy content before they are sent to the turbine 4I.

The above description of the invention as specically applied to the control of the transformof the evolved heat of reaction during the excthermic period lby the heat exchange fluid in order to permit the temperature of the contact material to rise to a desired degree by storing a portion of theevolved heat therein, after a predetermined time starting the endothermic reaction and utilizing a portion of the heat stored in the mass to provide heat during the reaction period and extracting the remainder of the stored heat from the contact material by the heat exchange fluid, then adjusting the heat exchange fluid to the aforesaid constant temperature before again beginning the cycle of operation.

3. In the treatment of fluid reactants in the presence of solid adsorptive mass, the steps of maintaining said mass in a cycle of operation involving an endothermic reaction with on-stream in liquid phase under the reaction conditions during the cycle in indirect heat exchange relation with the mass and at a constant temperature below that of the reactions, withdrawing only a portion of the evolved heat of reaction,

during the exothermic reaction by the heat exchange medium in order to permitthe mass to rise in temperature during this reaction and store the remainder of the evolved heat therein and after a predetermined period of time stopping the exothermic reaction and starting the endothermic reaction and during this reaction utilizing the stored heat to supply the heat of A reaction.

during the cycle in indirect heat exchange relation with the mass and at a constant temperature below that of the reactions, withdrawing only a portion of the evolved heatv of reaction during the exothermic reaction by the heat exchange medium in order to permit the mass to rise in temperature and store the remainder of the evolved heat therein and after a predetermined time stopping the exothermic reaction and starting the endothermic reaction and during this reaction utilizing the stored heat to supply the heat of reaction, withdrawing a'desired portion of the heat exchange medium and passing it in heat exchange relation with one of the reactants in order to extract heat from the medium and returning said portion to the main body of the medium in order to adjust the temperature of the main body to the aforesaid constant temperature, 'A

5. In the treatment of fluid reactants in the presence of solid adsorptive mass, the steps of maintaining said mass in a cycle of operation involving an endotherrnic reaction with on-stream reactants to effect the desired treatment alternating with an exothermic reaction with regeneration reactants to remove combustible deposits which accumulate on the mass during the sired temperaturerfor effecting the reactions which comprises supplying a heated gaseous medium to the manifolds for passage through the contact material in direct heat exchange relation therewith and through confined passageways in indirect heatexchange relation with the contact material, gradually increasing the temperature of the gaseous medium and continuing its circulation until the converters and contact material are preliminarily heated, cutting oi the iiow of gaseous .medium and supplying a heat exchange fluid to one of the manifolds for passage in indirect heat exchange relation with the contact material, gradually raising the temperature of said fluids and continuing their circulation through the contact mass until the contact material and converters are heated to approximately the temperature of the desired on-stream reaction, cutting off the flow of the gaseous me` dium and circulating the heat exchange fluid at about the lower limit of the on-stream temperature in order to substantially constantly withdraw heat from the contact material during a cycle of operations.

on stream period,vcirculating a body of heat exchange medium during the cycle which will remain substantially in liquid phase under the reaction conditions in indirect heat exchange relation with the mass and at a constant temperature below that of the reactions, withdrawing only a portion of the evolved heat of reaction during the exothermic reaction by the heat exchange medium in order to permit the mass to rise in temperature and store the remainder of the evolved heat therein and after a predetermined time stopping the exothermic reaction and starting theendothermic reaction and during this reaction utilizing the stored heat to supply the heat of reaction, withdrawing a desired portion of the heat exchange medium and passing it in parallel streams in heat exchange relation with other fluids including at least one of the reactants in order toextract heat from the medium and returning-said portion to the main body of the medium in order to adjust the temperature of the main body to the aforesaid constant temperature.

6. In theA use of one or more converters each having a reaction chamber and manifolds 4in communication therewith, wherein each reaction chamber contains contact material which is employed in cyclic operation involving alternate on-stream and regeneration reactions and a heat exchange fluid is circulated to control the temperature of the reaction, the method of heating up the converters and contact material to de- 7. In the use of one or more converters each having a reaction chamber and manifolds in communication therewith, wherein each reaction chamber contains contact material which is employed in a cycle of operations involving alternate reaction periods of greater and lesser heats of reaction, and a heat exchange fluid is circulated tocontrol the temperature of the reactions, the process of heatingA up the converters and contact material todesired temperature for effecting the alternate reactions which comprises heating a gaseous medium and supplying it to the manifolds for passagethrough the contact material in direct heat exchange relation therewith and for passage through confined passageways in indirect heat exchange relation with the contact material, gradually increasing the temperature of the gaseous medium and continuing its circulation until the converters and contact material are preliminarily heated, cutting ofi the passage of the gaseous medium to one of the manifoldsand supplying thereto a heat exchange medium in heated condition for passage in indirect heat exchange relation with thecontact material, continuing the supply' of the gaseous medium and the heat exchange medium to the manifolds and gradually increasing their temperatures until the' converters and contact material reach approximately the temperature of the lower temperature period of the cycle.

8. In the use of one or more converters each having a reaction chamber and manifolds in communication therewith, wherein each reaction chamber contains contact material which is employed in a cycle of operations involving alternate regeneration and ori-stream reactions'carried out at higher and lower temperatures, respectively, and a heat exchange medium is circulated to control the temperature of the reactions, the process of heating 'up the contact material and converters to desired temperature for effecting the alternate reactions which comprises heating a gaseous medium and supply it to the manifolds for passage through the contact material in direct heat relation therewith and for passage through conned passageways in indirect heat exchange relation with the contact material, gradually increasing the temperature of the gaseous medium and continuing its circulation until the converters and contact material are preliminarily heated, cutting oli the passage of the gaseous medium to one of the manifolds and supplying thereto a liquid heat exchange medium in heated condition for passage in indirect heat exchange relation with the contact material, continuing the passage of the gaseous medium and the liquid medium and gradually increasing their temperatures until the contact material and converters reach approximately the temperature 4 spectively, and a heat exchange medium is circulated during the lower temperature period of the cycle, the process of heating up the contact material and converters to desired temperature for effecting the alternate reactions which comprises heating a gaseous medium and supplying it to the manifolds for passage through the contact material in direct heat relation therewith and for passage through coniined passageways in indirect heat exchange relation with the contact material, gradually increasing the temperatures of the gaseous medium and continuing its circulation until the converters and contact material are preliminarily heated to a temperature substantially below the temperature of .the onstream reaction period, cutting off the passage of the heated gaseous medium to one oi' the manifolds and supplying thereto heat exchange medium for passage in indirect heat exchange relation with the contact material and comprising a fused mixture of nitrates and nitrites heatedabove 250 F. to place it in the liquid state, continuing the passage of the gaseous medium and the liquid heat exchange medium, gradually increasing their temperatures until the contact material and converters reach approximately the temperature of the on-stream period of the cycle.

10. In the use of one cr more converters each having a reaction chamber and manifolds in communication therewith, wherein each reaction chamber contains contact material which is employed in a cycle of operations involving alternate periods of higher and lower temperature reactions and a heat exchange medium is circulated to control the temperature of the reactions, the process of heating up the contact material and converters to desired temperature for effecting the alternate reactions which comprises heating a gaseous medium and supplying it to the manifolds for passage through the contact material in direct heat relation therewith and for passage through confined passageways in indirect heat exchange relation with the contact material, gradually increasing the temperature of the gaseous medium and continuing its circulation until the converters and contact material are preliminarily heated to a temperature substantially below the temperature of the lower temperature reaction period,a cutting off the passage of the heated gaseous medium to one of the manifolds and supplying thereto a heat exchange liquid having greater heat conductivity than the gaseous medium for passage in indirect heat exchange relation with the contact material, heating the gaseous iiuid to approximately the temperature of the lower temperature period of the cycle and passing it in heat exchange relation with the heat exchange liquid to give up heat thereto, then continuing the passage of the gaseous medium and the liquid medium at gradually, increased temperatures until the converters and contact material reach approximately the temperature of the lower temperature period of the cycle.

.JAMES W. HARRISON.

'THOMAS B. PRICKE'I'I. 

